Chemical conversion apparatus and method

ABSTRACT

Improved apparatus for carrying out catalytic chemical conversion and restoring the catalytic activity of solid particles previously used to promote chemical conversion involve improved devices to at least partially separate solid particles-vapor mixtures. These improved devices include, for example, properly positioned arresting vanes, flow reversal systems and/or plates, and provide for reduced attrition of the solid catalyst particles. 
     Improved methods employing such apparatus are also disclosed.

This invention relates to improved apparatus and methods for carryingout chemical conversions and for restoring the catalytic activity ofsolid particles used to promote chemical conversions. More particularly,the invention relates to such improved apparatus and methods forcarrying out chemical conversions and for restoring the catalyticactivity of solid particles used to promote such conversions whereinmixtures of solid particles and vapor require separation.

In many instances throughout the process industries, chemical reactionsoccur which are promoted by relatively small, e.g., diameters rangingfrom about 10 to about 500 microns, catalyst particles, for example, influidized bed reactors. One process involving such catalyst particles isthe catalytic cracking of higher boiling hydrocarbons to gasoline andother lower boiling components which is used extensively in thepetroleum industry. Often, apparatus used for carrying out such chemicalconversion, e.g., cracking, of a feedstock, e.g., hydrocarbon gas oil,involves a reaction zone where the relatively small catalyst particlesand feedstock are contacted at chemical conversion, e.g., hydrocarboncracking, conditions to form at least one chemical conversion product,e.g., hydrocarbons having a lower boiling point than the hydrocarbonfeedstock. Often, while promoting the desired chemical conversion, thecatalyst particles have deposited thereon material, e.g., carbon, cokeand the like, which acts to reduce the catalytic activity of theseparticles. Apparatus which are used to restore the catalytic activity ofsuch particles often include a regeneration zone where thedeposit-containing solid particles are contacted with oxygen-containingvapor at conditions to combust at least a portion of the depositmaterial.

Operation of both of the systems referred to above involves theformation of a mixture of solid particles and vapor which requiresseparation. Therefore, both the apparatus for carrying out chemicalconversion and the apparatus for restoring the catalytic activity of thesolid catalyst particles include a separation zone wherein the mixtureof solid particles and vapor formed in the reaction and regenerationzone, respectively, are at least partially separated. Such separationzones often involve conventional cyclone precipitators.

However, processing solid catalyst particles through such cycloneprecipitators causes increased particle attrition. That is, the solidcatalyst particles have an increased tendency to fall apart and/or formfines while being processed through a separation system, e.g., cycloneprecipitator. The resulting particle "fines" are often of such a sizethat they cannot be reused to promote chemical conversion. Clearly, itis advantageous to provide for reduced attrition of solid catalystparticles.

Therefore, one object of the present invention is to provide apparatusand methods for carrying out chemical conversion, e.g., cracking, of afeedstock, e.g., hydrocarbon, using solid catalyst particles whereinattrition of the particles is reduced.

Another object of the present invention is to provide apparatus andmethods for restoring the catalytic, e.g., hydrocarbon cracking,activity of solid catalyst particles wherein attrition of the particlesis reduced. Other objects and advantages of the present invention willbecome apparent hereinafter.

In one embodiment, the present invention involves an improved apparatusfor carrying out chemical conversion of a feedstock. This apparatusincludes a chemical reaction zone wherein the feedstock, e.g., asubstantially hydrocarbon gas oil, is contacted with solid particlescapable of promoting chemical conversion, e.g., hydrocarbon cracking, atchemical conversion conditions to form at least one chemical conversionproduct and a mixture of solid particles and vapor, the major portion,preferably at least about 90%, by weight of the solid particles havingdiameters in the range from about 10 to about 500 microns, preferablyfrom about 20 to about 200 microns; and at least one separation means influid communication with the reaction zone, wherein the mixture of solidparticles and vapor is at least partially separated. The separationmeans comprises a chamber defined by an interior cylindrical surface; aninlet means to the chamber in fluid communication with both the reactionzone and the chamber to allow entry of the solid particles-vapor mixtureto the chamber, wherein movement of the mixture causes solid particlesto preferentially move toward the cylindrical surface; a particle outletmeans from the chamber to allow at least a portion of the solidparticles of the mixture to exit the chamber; and a fluid outlet meansfrom the chamber to allow at least a portion of the vapor component ofthe mixture to exit from the chamber. In one embodiment, the presentimprovement involves arresting means located in spaced relation to, andpreferably attached to, the interior cylindrical surface to slow thevelocity of at least a portion of the solid particles as the solidparticles preferentially move toward the cylindrical surface, therebyinhibiting the attrition of the solid particles.

An improved method of chemical conversion, e.g., hydrocarbon cracking,utilizing such improved apparatus has also been discovered.

In an additional embodiment, the present invention involves an apparatusfor restoring the catalytic activity of solid particles which havepreviously been used to promote chemical conversion, e.g., hydrocarboncracking, and have deactivating carbonaceous deposit material thereon,the major portion, preferably at least about 90%, by weight of the solidparticles having diameters in the range from about 10 to about 500microns, preferably from about 20 to about 200 microns. This apparatusincludes a regeneration zone wherein the deposit-containing solidparticles are contacted with oxygen-containing vapor under conditions tocombust at least a portion of the deposit material and form a mixture ofsolid particles and vapor; and at least one separation means in fluidcommunication with the regeneration zone wherein the solidparticles-vapor mixture is at least partially separated. The separationmeans comprises a chamber defined by an interior cylindrical surface; aninlet means to the chamber in fluid communication with both theregeneration zone and the chamber to allow entry of the mixture to thechamber wherein movement of the mixture in the chamber causes solidparticles to preferentially move toward the cylindrical surface; aparticle outlet means from the chamber to allow at least a portion ofthe solid particles of the mixture to exit from the chamber; and a fluidoutlet means from the chamber to allow at least a portion of the vaporcomponent of the mixture to exit from the chamber. The presentimprovement provides for arresting means located in spaced relation to,and preferably attached to, the interior cylindrical surface to slow thevelocity of at least a portion of the solid particles as the solidparticles preferentially move toward the cylindrical surface, therebyinhibiting the attrition of the solid particles.

An improved method for restoring the catalytic activity of solidparticles utilizing this improved apparatus has also been found.

Each of the arresting means described above preferably involves aplurality of vanes, each of which vanes is attached to the interiorcylindrical surface and extend a distance, more preferably asubstantially equal distance, toward the central axis of the chamber.Thus, in a more preferred embodiment, the end of each of the vanes awayfrom the interior cylindrical surface is at a substantially equaldistance from the central axis of the chamber. These vanes form channelsor spaces through which at least a portion of the solid particlespreferentially moving toward the cylindrical surface flow. Further, thevanes are preferably positioned so that each vane overlaps at least oneadjacent vane when viewed from the central axis of the chamber.

A still further preferred embodiment involves arresting means comprisingsuch a plurality of vanes each of which is inclined at a predetermined,more preferably a substantially uniform, angle relative to the centralaxis of the chamber. The angle of incline is chosen so that theresistance to flow of the mixture of solid particles and vapor in thechamber is reduced. In other words, the vanes are preferably inclined inthe general direction of spiralling flow of this mixture past the vanesto reduce the flow resistance caused by these vanes. The inclined vanesalso act to urge solid particles in the proximity of the cylinricalsurface of the chamber downwardly and, thus, provide improved solidparticle-vapor separation. This feature of the present inventionprovides additionally improved solid particle attrition inhibition.

The relative sizes of the components of the present apparatus may bevaried depending on the particular application involved. For example,the reaction zone and regeneration zone may each have a volume rangingfrom about 10 cubic feet or less to about 100,000 cubic feet or more,preferably from about 100 to about 50,000 cubic feet. The chamber of thepresent separation means typically may have an inside diameter rangingfrom about 0.1 to about 10 feet or more, preferably from about 1 toabout 7 feet, and a length ranging from about 0.5 to about 50 feet ormore, preferably from about 5 to about 35 feet.

The apparatus of the present invention include at least one separationmeans. However, often the apparatus involves a plurality, morepreferably from about 3 to about 15, of such separation means in directfluid communication with either the reaction zone or the regenerationzone. "Direct fluid communication" as used herein refers tocommunication wherein the mixture of solid particles and vapor flowsdirectly from the reaction zone, or regeneration zone into theseparation means. This is in contrast to the situation wherein stagedseparators, e.g., two or more separation means in series, are employed.The second and following separation means, if any, in series are not indirect fluid communication with the reaction zone or regeneration zone.However, the present improved separation means may advantageously beused as either the first and/or succeeding separation means in such aseries.

The inlet means of the present separation means may involve a conduit influid communication with both the reaction zone, or regeneration zone,and the chamber. Although the conduit may empty into the chamber fromany convenient angle, preferably this conduit empties substantiallyparallel to the central axis of the chamber, e.g., top inlet to achamber situated so that its central axis is substantially vertical, orsubstantially tangential to the interior cylindrical surface of thechamber.

When entry to the chamber from the conduit is substantially parallel tothe central axis, the inlet means, for example, may further compriseflow directing means located in spaced relation to the interiorcylindrical surface and acting to direct the flow of the solidparticles-vapor mixture in the chamber so that at least a portion ofsolid particles preferentially move toward the cylindrical surface. In apreferred embodiment, the flow directing means involve a pair of partialbaffles situated, e.g., at mutually inclined angles, so that as themixture of solid particles and vapor from the conduit passes thebaffles, the mixture is caused to flow in a generally spiralling paththrough the chamber.

The present separation means may include flow redirecting means,preferably a pair of partial baffles in spaced relation, e.g., attached,to the interior cylindrical surface at a distance along this cylindricalsurface, e.g., below the inlet means, to redirect the flow of themixture of solid particles and vapor in the chamber in a generallyspiralling fashion through the remainder of the chamber. Such flowredirecting may be employed in the present separation means regardlessof the angle at which the solid particles-vapor mixture enters thechamber from the inlet means even when the conduit of the inlet meansempties substantially tangentially to the interior cylindrical surfaceof the chamber.

In one preferred embodiment, the present separation means furthercomprises velocity altering means. Such means preferably involve atleast one pair of partial baffles located in spaced relation, e.g.,attached, to the interior cylindrical surface below the inlet means.This pair of baffles is situated, e.g., at mutually inclined angles, sothat as the mixture of solid particles and vapor passes the baffles, thebaffles change, preferably increase, the radial component of thevelocity of the mixture. The angle of incline between the partialbaffles primarily determines the magnitude of the radial velocitycomponent, all other things being equal. The greater the angle ofincline between the partial baffles (in other words the more horizontalthe baffles in a vertical chamber), the greater the radial velocitycomponent. Improved separation of solid particles and vapor is achievedat increased radial velocities. However, such increased velocities tendto increase particle attrition. Therefore, the present apparatusinvolving at least one velocity altering means preferably provides forseparation of a portion, preferably a major portion, of the solidparticles at relatively low radial velocities, e.g., before the mixtureof solid particles and vapor pass the velocity altering means. Increasedradial velocities allow improved separation of the particles from theremaining mixture. Thus, the improved apparatus described above providesimproved separation while, at the same time, inhibiting solid particleattrition.

In a still further preferred embodiment, the inlet means involves atleast one flow reversal means in fluid communication with both thereaction zone or regeneration zone and the inlet conduit. The flowreversal means acts to substantially change, preferably substantiallyreverse, the direction of flow of the mixture of solid particles andvapor prior to this mixture entering the conduit. Such change,preferably reversal, in the direction of flow of this mixture causes aportion of the solid particles to separate from the mixture. Since theseseparated particles are not subjected to the attrition causingconditions in the chamber of the separation means, overall particleattrition is reduced. In this embodiment, the present apparatuspreferably includes particle withdrawal means in fluid communicationwith the flow reversal means which allows at least a portion of thesolid particles separated in the flow reversal means to be withdrawn. Inone embodiment, the particle withdrawal means is in fluid communicationwith the particle outlet means of the present separation means so thatthe separation means provides a single stream of separated particles. Ofcourse, the withdrawal means need not be so connected. Although thepresent flow reversal means is particularly useful in separation meansincluding the present arresting means, such arresting means need not beincluded. Even without such arresting means, a separation means whichincludes the present flow reversal means provides substantial catalystparticle attrition inhibition.

Although the present invention is useful in many chemical conversionsand catalyst regenerations, these apparatus and methods find particularapplicability in systems for the catalytic cracking of hydrocarbons andthe regeneration of catalysts so employed. Such catalytic hydrocarboncracking often involves converting, i.e., cracking, heavier or higherboiling hydrocarbons to gasoline and other lower boiling components,such as hexane, hexene, pentane, pentene, butane, butylene, propane,propylene, ethane, ethylene, methane and mixtures thereof. Often, thesubstantially hydrocarbon feedstock comprises a gas oil fraction, e.g.,derived from petroleum, shale oil, tar sand oil, coal and the like. Suchfeedstock may comprise a mixture of straight run, e.g., virgin, gas oil.Such gas oil fractions often boil primarily in the range from about 400°to about 1000° F. Other substantially hydrocarbon feedstocks, e.g.,other high boiling or heavy fractions of petroleum, shale oil, tar sandoil, coal and the like, may be cracked using the apparatus and method ofthe present invention. Such substantially hydrocarbon feedstock oftencontain minor amounts of contaminants, e.g., sulfur, nitrogen and thelike.

Hydrocarbon cracking conditions are well known and often includetemperatures from about 850° to about 1100° F., preferably from about900° to about 1050° F. Other reaction conditions usually includepressures of up to about 100 psig.; catalyst to oil ratios of from about5 to 1 to about 25 to 1; and weight hourly space velocities of fromabout 3 to about 60. These hydrocarbon cracking conditions are notcritical to the present invention and may be varied depending, forexample, on the feedstock and catalyst being used and the productwanted. The hydrocarbon cracking reaction is generally conducted in theessential absence of added free molecular hydrogen.

In addition, the catalytic hydrocarbon cracking system includes anapparatus for restoring the catalytic activity of catalyst particlespreviously used to promote hydrocarbon cracking. This apparatus involvesa catalyst regeneration zone into which at least a portion of thecatalyst from the cracking reaction zone is withdrawn. Such catalyst iscontacted with free oxygen-containing gas in the regeneration zone torestore or maintain the activity of the catalyst by removing, i.e.,combusting, carbonaceous material deposited on the catalyst particles.The combustion gas temperature in the regeneration zone is generallyfrom about 900° to about 1500° F., preferably from about 900° to about1300° F. and more preferably from about 1100° to about 1300° F. At leasta portion of the regenerated catalyst is often returned to thehydrocarbon cracking reaction zone.

The catalyst particles useful in the catalytic hydrocarbon crackingembodiment of the present invention may be any conventional catalystcapable of promoting hydrocarbon cracking at the conditions present inthe reaction zone, i.e. hydrocarbon cracking conditions. Similarly, thecatalytic activity of such particles is restored at the conditionspresent in the regeneration zone. Typical among these conventionalcatalysts are those which comprise alumina, silica, silica-alumina, atleast one crystalline alumino silicate having pore diameters of fromabout 8 to about 15A and mixtures thereof. Because of the increasedeconomic incentive for maintaining the particle size ofzeolite-containing catalyst, it is preferred that the catalyst particlescomprise from about 1 to about 50%, more preferably from about 5 toabout 22%, by weight of at least one crystalline alumino-silicate havinga pore diameter of from about 8 to about 15A. At least a portion of thealumina, silica, silica-alumina and crystalline alumino-silicate may bereplaced by clays which are conventionally used in hydrocarbon crackingcatalyst compositions. Typical examples of these clays includehalloysite or dehydrated halloysite (kaolinite), montmorillonite,bentonite and mixtures thereof. These catalyst compositions may alsocontain minor amounts of other inorganic oxides such as magnesia,zirconia, etc. When the catalyst particles contain crystallinealumino-silicate, the compositions may also include minor amounts ofconventional metal promotors such as the rare earth metals, inparticular, cerium. Such catalyst compositions are commerciallyavailable in the form of relatively small particles, e.g., havingdiameters in the range from about 20 to about 200 microns, preferablyfrom about 20 to about 150 microns. In general, and except as otherwiseprovided for herein, the apparatus of the present invention may befabricated from any suitable material or combination of materials ofconstruction. The material or materials of construction used for eachcomponent of the present apparatus may be dependent upon the particularapplication involved. Of course, the apparatus should be made ofmaterials which are substantially unaffected, except for normal wear andtear, by the conditions at which the apparatus are normally operated. Ingeneral, such material or materials should have no substantialdetrimental effect on the feedstock being chemically converted, thechemical conversion product or products or the catalyst being employed.

These and other aspects and advantages of the present invention are setforth in the following detailed description and claims, particularlywhen considered in conjunction with the accompanying drawings in whichlike parts bear like reference numerals.

In the drawings:

FIG. 1 is a simplified schematic view of a fluid bed catalytichydrocarbon cracking reactor-regeneration system.

FIG. 2 is a partial side elevation view, partly in section, of oneembodiment of the separation means shown in FIG. 1.

FIG. 3 is a section view of the embodiment shown in FIG. 2 taken alongline 3--3.

FIG. 4 is a partial side elevation view, partly in section, of anotherembodiment of the separation means shown in FIG. 1.

FIG. 5 is a top elevation view of the embodiment shown in FIG. 4.

FIG. 6 is a partial side elevation view, partly in section, of a furtherembodiment of the separation means shown in FIG. 1.

FIG. 7 is a section view of the embodiment shown in FIG. 6 taken alongFIG. 7--7.

FIG. 8 is a partial side elevation view, partly in section, of onealternative embodiment of the present improved separation means.

FIG. 9 is a section view of the embodiment shown in FIG. 8 taken alongFIG. 9--9.

Referring now to the drawings, FIG. 1 shows a simplified schematicdiagram of a catalytic hydrocarbon cracking reactor-regenerator system.Although the drawings and following description are directedparticularly to catalytic hydrocarbon cracking, the present inventionmay be readily adapted to apparatus and methods for other chemicalconversions and catalyst regenerations by those skilled in the art. InFIG. 1, reactor 10 provides the required space for catalytic hydrocarboncracking to occur. Preheated hydrocarbon feedstock, e.g., petroleumderived gas oil, from line 12 is combined with catalyst particles, e.g.,more than 90% by weight of such particles having diameters in the rangefrom about 30 to about 100 microns, from line 14. The mixture offeedstock and catalyst flows through riser 16 (where a portion of thecatalytic hydrocarbon cracking takes place) into reactor 10. Thefeedstock (and certain cracked products) form a "dense fluid bed" belowlevel 18. The solid particles-vapor, e.g., cracked products andunreacted feedstock, mixture in reactor 10 above level 18 is in the formof a "lean fluid". This "lean fluid" enters first separator 20tangentially through inlet 22. First separator 20 acts, as will bedescribed in detail hereinafter, to separate a portion of the solidparticles in the "lean fluid" from the remainder of the solid catalystparticles-vapor mixture, which is sent through line 24 to secondseparator 26. The separated solid particles from first separator 20 flowthrough first dip leg 28 to the "dense fluid bed" below level 18. Thesolid particles-vapor mixture in line 24 is conveyed to the top ofsecond separator 26 which acts to further separate solid particles fromthe vapor. Vapor from second separator 26 exits through line 30 and issent to product processing, e.g., fractionation, other chemicalreactions and the like, to produce a final saleable product. The vaporin line 30 may also require additional processing to remove anyremaining solid particles, e.g., by conventional means well known in theart. The separated solid particles leave second separator 26 by seconddip leg 32 which exits below level 18.

Solid particles are withdrawn from reactor 10 through first stripper 34.Stripping gas, e.g., steam, from line 36 enters first stripper 34 andacts to strip hydrocarbon from the solid particles exiting reactor 10.The stripped solid catalyst particles from first stripper 34 flowthrough line 38, past valve 40, through line 42 and are combined with anoxygen-containing gas, e.g., air, from line 44. The mixture of solidcatalyst particles, which include carbonaceous deposit material formedin reactor 10, and oxygen-containing gas flow through pipe 46 intoregenerator 48 where at least a portion of the carbonaceous depositmaterial on the solid catalyst particles is removed by combustion withthe oxygen-containing gas. The "lean fluid" above the level 50 inregenerator 48 is a mixture of solid catalyst particles and vapor. This"lean fluid" enters third separator 52 via top inlet 54. Third separatoracts to separate solid catalyst particles, which exit third separator 52through third dip leg 56, from the vapor which exits the third separator52 through outlet line 58. The vapor from line 58, which includescombustion flue gases, may be released to the atmosphere or furtherprocessed, for example, in an electrostatic precipitator, to remove anyremaining solid particles.

Regenerated catalyst solid particles, i.e., catalyst particles whichhave had catalytic activity at least partially restored by removal ofcarbonaceous deposit material, are removed from regenerator 50 throughstandpipe 57. As the solid catalyst particles flow through standpipe 57,fluidizing gas, e.g., steam, from line 60 enters standpipe 57, contactsthe solid particles, thereby fluidizing the solid particles in standpipe57 and acting to strip any remaining oxygen-containing gas from thesolid particles. The thus fluidized and stripped solid catalystparticles flow from standpipe 57 through line 62, past valve 64 and intoline 14. The solid catalyst particles from line 14 are combined with thehydrocarbon feedstock from line 12 and the cycle is repeated.

Referring now to FIGS. 2 and 3, first separator 20 is shown in moredetail. First separator 20 is defined by hollow cylinder 66, which hasan interior cylindrical surface 67, cone shaped hopper 68, line 24, dipleg 28 and vanes 70. Inlet 22 is situated to allow substantiallytangential entry of the solid particles-vapor mixture into firstseparator 20. Inlet 22, line 24 and dip leg 28 act as described above.The solid particles-vapor mixture from inlet 22 is caused to flow in agenerally spiralling downwardly fashion through a portion of the spacedefined by the hollow cylinder 66. Such flow results in the solidparticles preferentially moving toward the interior cylindrical surface67. Vanes 70 are attached, e.g., welded, to the interior cylindricalsurface 67. Vanes 70 act to slow the solid particles as theypreferentially move toward interior cylindrical surface 67, thusreducing the impact force encountered by the solid particles hittinginterior cylindrical surface 67.

As shown in FIGS. 2 and 3, each of the vanes 70 runs substantially theentire length of hollow cylinder 66 and are of substantially uniformwidth. The ends of the vanes 70 away from interior cylindrical surface67 extend a substantially uniform distance into the space defined byhollow cylinder 66. In other words, each of the vanes 70 is disposed ata substantially uniform angle relative to the hollow cylinder 66. Inaddition, each of the vanes 70 overlaps at least one other vane 70.Thus, the vanes 70 form corridors, or channels, for the passage of solidparticles as they preferentially move toward the interior cylindricalsurface 67. As the solid particles approach the interior cylindricalsurface 67, gravity acts to force the particles down along the side ofinterior cylindrical surface 67, into hopper 68 and then into first dipleg 28. Catalyst particles in first dip leg 28 form a vapor seal so thatvapor in first separator 20 is substantially prevented from exitingthrough first dip leg 28. Instead, such vapor is removed from firstseparator 20 through line 24. This vapor also includes solid particlesat least a portion of which are to be removed in the second separator26.

The second separator 26 is shown in more detail in FIGS. 4 and 5. Themixture of solid catalyst particles and vapor exiting first separator 20flows through line 24 and enters through the top of second separator 26.Second separator 26 is defined by hollow cylinder 72, which has aninterior cylindrical surface 73, conical hopper 74, second dip leg 32,and outlet line 30. Also included are inclined vanes 75 and a singlepair of partial baffles 76 and 78. Each of the inclined vanes 75 isattached, e.g., welded, to the interior cylindrical hollow surface 73.Each of the partial baffles 76 and 78 is attached, e.g., welded, tooutlet line 30.

The partial baffles 76 and 78 are situated so as to cause the solidparticles-vapor mixture entering the top of second separator 26 to flowin a generally spiralling fashion generally downwardly through a portionof the space defined by the hollow cylinder 72. As this solidparticles-vapor mixture flows in such a manner in the hollow cylinder72, at least a portion of the solid particles preferentially move towardthe interior cylindrical surface 73. Inclined vanes 75 act to slow thevelocity of the solid particles as they preferentially move toward theinterior cylindrical surface 73, thus cushioning the impact of thesesolid particles with the interior cylindrical surface 73 and reducingthe amount of break-up or attrition of such solid particles.

Each of the inclined vanes 75 is inclined at a substantially uniformangle, with respect to the central axis of hollow cylinder 72, in thegeneral direction of the spiralling downwardly flow of the solidparticles-vapor mixture in the proximity of the inclined vanes 75. Suchinclination of vanes 75 has been found to reduce the resistance to flowof the solid particles-vapor mixtures through hollow cylinder 72, toprovide improved separation of the solid catalyst particles and thevapor, and to result in still further reduction in the attrition of thesolid catalyst particles. As indicated in FIG. 4, inclined vanes 75 arepresent in several rows. Such configuration is useful because of ease offabrication. However, such configuration is not an essential feature ofthe present invention. Thus, in this embodiment, any placement of theinclined vanes 75 is suitable and within the scope of the invention,provided that such inclined vanes 75 are inclined in the generaldirection of spiralling downwardly flow of the solid particles-vapormixture in the proximity of the inclined vanes 75, and further providedthat such inclined vanes 75 act to reduce the velocity of the solidparticles moving preferentially toward the interior cylindrical surface73.

Second separator 26 functions as follows. The mixture of solid particlesand vapor enters hollow cylinder 72 from line 24. As this mixture flowspast the pair of partial baffles 76 and 78, the solid particles andvapor are caused to flow in a generally spiralling fashion generallydownwardly through a portion of the space defined by hollow cylinder 72.At least a portion of the solid particles in the mixture are caused topreferentially move toward the interior cylindrical surface 73 of hollowcylinder 72. As solid particles approach interior cylindrical surface73, gravity causes these particles to fall into conical hopper 74 andthen into second dip leg 32. The solid particles in second dip leg 32act as a vapor seal so that the vapor in hollow cylinder 72 is caused toexit through outlet line 30. In this fashion, the solid particles-vapormixture entering hollow cylinder 72 is at least partially separated.

Third separator 52 is shown in more detail in FIGS. 6 and 7. Thirdseparator 52 is defined by hollow cylinder 80, having an interiorcylindrical surface 81, top inlet 54, hopper 82, third dip leg 56 andoutlet line 58. Third separator 52 also includes two pair of partialbaffles 84 and 86 as well as 88 and 90. Each of these baffles isattached, e.g., welded, to outlet line 58. Partial plate 92 is attached,e.g., welded, to the interior cylindrical surface 81 of hollow cylinder80. Outlet 91 provides an intermediate outlet from hollow cylinder 80and is in fluid communication with third dip leg 56 through pipe 94.Third separator 52 also includes several rows of inclined vanes 96 eachof which is attached, e.g., welded, to the interior cylindrical surface81 of hollow cylinder 80.

Third separator 52 functions as follows. The solid particles-vapormixture from regenerator 48 enters the interior of hollow cylinder 80through top inlet 54. As this mixture passes partial baffles 84 and 86,the mixture of solid particles and vapor is caused to flow in agenerally spiralling fashion generally downwardly through a portion ofthe space defined by hollow cylinder 80. Such movement causes at least aportion of the solid particles to preferentially move toward theinterior cylindrical surface 81 of hollow cylinder 80. Inclined vanes 96act to reduce the velocity of these solid particles as they approach theinterior cylindrical surface 81 of hollow cylinder 80. As solidparticles approach interior cylindrical surface 81, gravity causes suchparticles to fall onto partial plate 92. The spiralling motion of thevapor passing partial plate 92 causes at least a portion of the solidparticles on partial plate 92 to fall through pipe 94. The solidparticles in pipe 94 are conveyed to third dip leg 56. The remainingsolid particles and vapor from a mixture which flows past partialbaffles 88 and 90. Partial baffles 88 and 90 are inclined at a lesssevere angle (relative to the horizontal) than are partial baffles 84and 86. Thus, partial baffles 88 and 89 act to increase the radialcomponent of the velocity of the solid particles-vapor mixture. Suchincrease in the radial velocity increases the force acting upon thesolid particles to move such particles toward the interior cylindricalsurface 81 of hollow cylinder 80. Again, as these particles approachinterior cylindrical surface 81 of hollow cylinder 80, gravity acts toforce such solid particles down toward hopper 82 and into third dip leg56. The solid particles in third dip leg 56 provide a vapor seal so thatthe vapor in hollow cylinder 80 is forced through outlet line 58.

The embodiment of the present invention illustrated by third separator52 provides for intermediate removal of solid catalyst particles throughpipe 94 prior to increasing the radial velocity of the remaining solidparticles-gas mixture. Since these solid particles which are removedthrough pipe 94 are not subjected to increased radial velocities,attrition of such solid catalyst particles is reduced. Only after theseparticles are removed from hollow cylinder 80 through pipe 94 is theradial velocity of the remaining solid particles-gas mixture increasedby flowing past partial baffles 88 and 90. Increasing the radialvelocity of this remaining mixture acts to improve the degree ofseparation between the solid particles and vapor by the apparatus ofthis embodiment of the present invention. Thus, the present inventionprovides reduced solid particle attrition and increased separationefficiency.

The intermediate removal of solid particles from hollow cylinder 80through pipe 94 plus the increased radial velocity caused by partialbaffles 88 and 90 allows the third separator 52 to have a separatingcapacity approaching that of two separators in series, e.g., such asfirst separator 20 and second separator 26. Thus, an apparatus similarto third separator 52 may be used in reactor 10 in place of, or inconjunction with, first separator 20 and second separator 26. Forexample, if additional separation is desired in reactor 10, an apparatussimilar to third separator 52 may be used in series with first separator20 to replace second separator 26. Of course, apparatus similar to firstseparator 20 and/or second separator 26 may be used in series with or asa replacement for third separator 52 to separate the solid catalystparticles-vapor mixture from regenerator 48. Other combinations ofapparatus similar to first, second and third separators 20, 26, and 52may also be used in either reactor 10 and regeneratore 48 and all suchcombinations are within the scope of the present invention. In addition,first separator 20 may include a top inlet (rather than the tangentialinlet 22 shown) and also include at least one pair of partial baffles,such as partial baffles 76 and 78, to cause the solid particles-vapormixture to flow in a generally spiralling fashion generally downwardlythrough a portion of the space defined by hollow cylinder 66. Othermodifications regarding position of various components of the presentapparatus are also within the scope of the present invention.

Although FIG. 1 illustrates a single series of separators, i.e., firstand second separators 20 and 26 in series, and a single separator, i.e.,third separator 52, conventional reaction zones and regeneration zonesoften include a plurality of separators or series of separators. Forexample, reactor 10 and/or regenerator 48 may contain from about four toabout 12 parallel series of separators with from one to about threeseparators in each series. Each of the individual separators in each ofthese series may be constructed similarily to first, second or thirdseparators 20, 26, or 52. In any event, apparatus and methods involvingsuch plurality of separators or series of separators are within thescope of the present invention.

One additional embodiment of the present invention is shown in detail inFIGS. 8 and 9. The separator, referenced generally as 100, is defined byhollow cylinder 102, having an interior cylindrical surface 103, hopper104, dip leg 106 and vapor outlet line 108. Also included in separator100 are four corner pieces 110 which provide fluid communication betweenthe reactor 10 (or regenerator 48) and the interior of hollow cylinder102. Corner pieces 110, which are each attached, e.g., welded, to theoutside of hollow cylinder 102, are each in fluid communication with dipleg 106 through pipes 112. Each of the corner pieces 110 acts to causethe mixture of solid catalyst particles and vapor to reverse itsdirection of flow prior to entering the interior of hollow cylinder 102.Such flow reversal causes a portion of the solid particles to beseparated from the mixture prior to entering the interior of hollowcylinder 102. The solid particles which are separated in corner pieces110 suffer reduced attrition since, for example, such particles areseparated at conditions providing reduced attrition and are notsubjected to the conditions exiting within hollow cylinder 102.

Separator 100 functions as follows. The solid particles-vapor mixturefrom reactor 10 (or regenerator 48) enters the four corner pieces 110,as shown in FIG. 9. As this mixture passes through the corner pieces110, the flow of the mixture is reversed, thus causing a portion of thesolid catalyst particles to be separated. The separated solid catalystparticles fall through pipes 112 into dip leg 106. The remaining solidparticles-vapor mixture enters the interior of hollow cylinder 102.Because of the tangential entry of this mixture into the interior ofhollow cylinder 102, the mixture flows in a generally spiralling fashiongenerally downwardly through a portion of the space defined by thehollow cylinder 102. Such movement of the mixture causes solid particlesto preferentially move toward the interior cylindrical surface 103 ofhollow cylinder 102. As these solid particles approach the interiorcylindrical surface 103, gravity acts to force such particles downthrough hopper 104 into dip leg 106. The solid particles enter dip leg106 and act to form a vapor seal. The vapor in hollow cylinder 102 exitsthrough outlet line 108. In this manner, the solid particles-vapormixture entering separator 100 is separated.

Although not an essential component of the embodiment of the presentinvention illustrated in FIGS. 8 and 9, separator 100 may, andpreferably does, include arresting means, e.g., such as vanes 70 orinclined vanes 75. Also, separator 100 may include one or more pairs ofpartial baffles such as partial baffles 76 and 78, to alter the radialvelocity of the solid particles-vapor mixture in hollow cylinder 102.

Separator 100 may be used in conjunction with, or as a replacement for,first separator 20, second separator 26 or third separator 52. In anyevent, the apparatus illustrated by separator 100 and its use have beenfound to provide outstanding reduction in solid catalyst particleattrition.

The following examples clearly illustrate the present invention.However, these examples are not to be interpreted as specificlimitations on the invention.

EXAMPLES 1 to 4

These examples illustrate certain of the advantages of the presentinvention.

A device which propels a mixture of solid catalyst particles and air wasused to simulate the movement of solid catalyst particles in variousseparators.

This device involves a cylindrical chamber having an inside diameter of17 inches and a depth of 3 inches. Centrally mounted in the chamber isan impeller having four blades or paddles. The impeller has an overalldiameter of 10 inches and a depth of 1.375 inches. The impeller isdriven by a variable speed motor which is mounted above and outside thechamber. A series of eight baffles surround the impeller. Each of thesebaffles is 3 inches deep, 6 inches long and is welded to the interiorperipheral surface of the chamber. Each of the baffles extend from thissurface a substantially uniform radial distance of 3 inches into thechamber. Also, each of the baffles is situated at a substantiallyuniform acute angle relative to the tangent at the point of attachmentto the chamber.

A conical hopper, situated directly below the chamber, is in fluidcommunication with the chamber. A plate situated directly below andsubstantially co-extensive with the diameter of the impeller preventscatalyst particles from falling into the hopper before the particles areforced out radially beyond the impeller. A piece of flexible 1 inch O.D.tubing provides fluid communication between the bottom of the hopper andthe chamber. This tubing enters the chamber from below and terminates inthe space at the center of the impeller.

This device functions as follows. A quantity of catalyst particles, ofknown size distribution, is stored in the hopper. Air, from thesurrounding environment is allowed to mix with the particles. Thevariable speed motor is activated and causes the impeller to rotate.Such rotation creates forces causing the catalyst particles-air mixtureto flow through the tubing into the chamber. The impeller forces themixture in the chamber toward the peripheral interior surface of thechamber. At least a portion of the solid particles strikes this surface.In any event, substantially all of the solid particles are returned tothe hopper from the chamber and are recycled to the chamber through thetubing. After a period of time of operation, the solid catalystparticles in the hopper are analyzed for size to determine the degree ofparticle attrition which resulted from operation of the device.

In addition, a smooth cylindrical insert can be placed in the chamber.The perimeter of this insert is defined by the edges of the baffles awayfrom the interior peripheral surface of the chamber. The insert hassubstantially the same depth as the baffles. Operation of the devicewith this insert in place simulated the operation of a separator withoutarresting means, e.g., baffles, vanes and the like.

Velocities and mass circulation rates within the test device aredetermined as follows:

The rotations per minute (rpm) of the variable speed motor is accuratelymeasured by a strobe tachometer, which permits the calculation of thetangential component of velocity of the mixture of catalyst particlesand air leaving the impeller. The impeller is supported by the variablespeed motor, and contacted the chamber housing only through a feltwasher of negligible friction. The chamber housing is supported from aball bearing, so that the torque caused by the circulation of air andcatalyst particles can be measured. A string, having a weight Msuspended therefrom, is attached to the chamber housing tangential tothe outer perimeter of the impeller. Force is calculated from thelateral displacement of the suspended weight using the followingequation: ##EQU1## wherein: X = the lateral displacement of the weightfrom the chamber housing

L = the length of the string

With the variable speed motor in operation, the air circulation isblocked off by closing the tubing with pinch clamps, and the forcecaused by friction and internal turbulence is measured. Then, the pinchclamps are removed, and the increase in force caused by circulating airis noted. Then, the catalyst is added and the incremental force causedby catalyst circulation is measured. Circulation rates of both air andcatalyst are calculated from tangential force and tangential velocity asfollows: ##EQU2## A catalyst particle undergoing radial acceleration bya rotating blade describes a logarithmic spiral, and will leave arotating blade of the impeller at an angle of 45° to the tangent so thatits radial and tangential velocities are equal, if it begins near thecenter and if there is no frictional drag against the blade. In thiscase, the coefficient of friction of the catalyst particles is knownfrom the angle of repose of a mass of such particles, so this can beused in the calculation of radial velocity. Tangential velocity of thecatalyst particles is calculated as follows:

V_(t) = 2πrw; where r is the radius of the vane and w is revolutions perunit time of the impeller. If the catalyst particles are introducedclose to the center of the impeller, the radial velocity of the catalystparticles is:

    V.sub.r = (√4 +α.sup.2 = α) πrw;

where α is the coefficient of friction of the catalyst. The totalvelocity of the catalyst particles will be the vector sum of thetangential and radial velocities:

    V = √ V.sub.t.sup.2 + V.sub.r.sup.2

Using a value of 0.45 for α, the net velocity is 1.26 times thetangential velocity.

The catalyst particles used in this test device were obtained from acommercial fluid bed catalytic hydrocarbon cracking reaction system.These particles had a composition which included about 15% by weight ofalumino-silicate in a binder comprising silica-alumina. Before operationof the test device, these solid particles had the following sizedistribution:

    ______________________________________                                        Size, Microns     % By Weight                                                 ______________________________________                                        120+              12.0                                                        100-120           18.0                                                         80-100           24.0                                                        60-80             23.0                                                        40-60             5.6                                                          0-20             1.5                                                         ______________________________________                                    

Approximately 20 grams of these catalyst particles were placed in thehopper of the test device prior to each test.

A series of four tests were run with the second of the motor set at 2300rpm. In three of these tests, the baffles remained uncovered, while inone test the smooth insert covered the baffles, as described above.Results of these tests were as follows:

    ______________________________________                                                                Catalyst                                                                             Total   Increment-                                   Con-     Total    Circu- Catalyst                                                                              al fines                                     figura-  Velocity,                                                                              lation,                                                                              Circulated                                                                            Production                             RUN   tion     Ft./Sec. gms./sec.                                                                            gms.    gms.*                                  ______________________________________                                        1     Baffles  127      9.2    8280    0.13                                         Un-                                                                           covered                                                                 2     "        127      12.8   11540   0.164                                  3     "        127      6.5    7790    0.15                                   4     Smooth   127      8.8    7940    0.88                                         Insert                                                                        In place                                                                ______________________________________                                         *Incremental Fines Production is defined as the net increase in particles     20 microns or less in size which is apparent in the mass of catalyst afte     each test.                                                               

These results indicate clearly that the separation means included in thepresent apparatus provides unexpected and substantial benefits. Forexample, when the test device described above was configured to simulatethe separation means of the present apparatus, i.e., runs 1, 2, and 3,incremental fines production was less than 20% the fines production withthe device configured to simulate a smooth wall cyclone separator, i.e.,run 4. Thus, the present apparatus and methods which involve separationmeans including arresting means surprisingly provide reduced catalystparticle attrition, e.g., relative to conventional separators.

EXAMPLE 5

A catalytic cracking system, configured as shown in FIG. 1, is employedto convert 20,000 barrels per day of fresh petroleum derived gas oil tolower boiling hydrocarbons. The catalyst employed in the system is acommercially available composition which included about 15% by weight ofan aluminosilicate in a binder comprising silicaalumina. This catalysthas a particle size distribution similar to the catalyst particles usedin Examples 1 to 4.

The weight ratio of catalyst particles to total (fresh plus recycle)hydrocarbon feed entering riser 16 is about 8 to 1. conditions withinreactor 10 are as follows:

    ______________________________________                                        Temperature, ° F.                                                                            930                                                     Pressure, psig        8                                                       WHSV                  15                                                      ______________________________________                                    

Such conditions result in about 75% by volume conversion of the gas oilfeedstock to products boiling at 400° F. and below. A mixture of solidcatalyst particles and hydrocarbon vapor enter each of six series ofseparators similar to first separator 20 and second separator 26, whichare employed in series as shown in FIG. 1. Such separators act toseparate solid catalyst particles from the hydrocarbon vapor, which ispassed to product processing. Such processing also provides a stream ofunreacted hydrocarbons, a portion of which is recycled and combined withfresh feedstock, and heated prior to entering riser 16 for furthercracking.

Catalyst particles from reactor 10 flow through stripper 34 into lines38 and 42 and are combined with the air stream from line 44. Thesecatalyst particles from reactor 10 have carbonaceous deposits thereon.Such catalyst particles include about 1.5% by weight of coke which is tobe at least partially combusted in regenerator 48.

Air in line 44 is heated so that the desired temperature withinregenerator 48 is maintained. The amount of air added to regenerator 48includes about 1.15 times the amount of oxygen theoretically required tocompletely combust the coke from the catalyst particles. Conditionsexisting within the regenerator 48 and at which combustion of thecarbonaceous catalyst deposits take place are as follows:

    ______________________________________                                        Temperature, ° F.                                                                            1150                                                    Pressure, psig.       8                                                       Average Catalyst                                                               Residence Time, Min. 12                                                      ______________________________________                                    

A mixture of solid catalyst particles and a gaseous phase, e.g.,uncombusted oxygen, combustion products, nitrogen, steam and the like,enter each of six separators similar to third separator 52 where suchmixture is at least partially separated.

Catalyst particles from regenerator 48 enter standpipe 57 and flowthrough lines 62 and 14 and are combined with hydrocarbon feedstock fromline 12 prior to entry into riser 16.

After a period of time in operation, it is determined that this systemprovides improved results, e.g., reduced catalyst particle attrition,relative to a similar reactor-regenerator system involving conventionalcyclone separators in place of the separators similar to first separator20, second separator 26 and third separator 52 of the system describedabove.

EXAMPLE 6

Improved results, e.g., reduced catalyst particle attrition relative toa system with conventional cyclone separators, are obtained usingvarious modifications of the reactor-regenerator system shown in FIG. 1to process 20,000 barrels per day of a fresh petroleum derived gas oil.The modifications which are used include (1) replacing one or both ofthe first and second separators 20 and 26 in reactor 10 with a devicesimilar to third separator 52 and/or a device similar to the separatordepicted in FIGS. 8 and 9. Another useful modification involvesreplacing the third separator 52 in regenerator 48 with a device similarto first separator 20 and/or second separator 26 and/or the separatordepicted in FIGS. 8 and 9. In any event, outstanding benefits, e.g.,reduced catalyst particle attrition, are achieved while using suchmodified systems.

While this invention has been described with respect to various specificexamples and embodiments, it is to be understood that the invention isnot limited thereto and that it can be variously practiced within thescope of the following claims.

The embodiments of the invention in which an exclusive property orprivilege is claimed and defined as follows:
 1. In an apparatus forcarrying out chemical conversion of a feedstock which includes achemical reaction zone wherein said feedstock is contacted with solidparticles capable of promoting said chemical conversion at chemicalconversion conditions to form at least one chemical conversion productand a mixture of solid particles and vapor, the major portion by weightof said solid particles having diameters in the range from about 10 toabout 500 microns; and at lease one separation means in fluidcommunication with said reaction zone wherein said mixture is at leastpartially separated, said separation means comprising a chamber definedby an interior cylindrical surface; an inlet means in fluidcommunication with both said reaction zone and said chamber to allowentry of said mixture to said chamber, said inlet means being situatedso that the movement of said mixture in said chamber causes solidparticles to preferentially move toward said cylindrical surface; afluid outlet means in fluid communication with said chamber to allow atleast a portion of said vapor component of said mixture to exit fromsaid chamber; and a particle outlet means in fluid communication withsaid chamber to allow at least a portion of said solid particles to exitfrom said chamber; the improvement which comprises:arresting meanslocated in spaced relation to said interior cylindrical surface to slowthe velocity of at least a portion of said solid particles as said solidparticles preferentially move toward said cylindrical surface, therebyinhibiting the attrition of said solid particles.
 2. The apparatus ofclaim 1 wherein said arresting means comprises a plurality of vanesattached to said cylindrical surface and which extend inwardly towardthe central axis of said chamber.
 3. The apparatus of claim 2 whereinsaid vanes which are mutually adjacent form a channel into which flowsat least a portion of said solid particles preferentially moving towardsaid cylindrical surface.
 4. The apparatus of claim 3 wherein said vanesare attached to said cylindrical surface and are positioned so that eachsaid vane overlaps at least one adjacent vane when viewed from thecentral axis of said chamber.
 5. The apparatus of claim 4 wherein eachof said vanes is inclined at an angle relative to said central axis ofsaid chamber to reduce the resistance to flow of said solid particlesand vapor in said chamber caused by said vanes.
 6. The apparatus ofclaim 5 wherein each of said vanes extend a substantially equal distanceinto said chamber so that the end of said vanes away from saidcylindrical surface is at a substantially equal distance from saidcentral axis of said chamber and each of said vanes is inclined at asubstantially uniform angle relative to said central axis of saidchamber.
 7. The apparatus of claim 1 wherein said inlet means includesat least one flow reversal means to substantially change the directionof flow of said mixture prior to said mixture entering said chamber tothereby cause at least a portion of said solid particles to be separatedfrom said mixture prior to said mixture entering said chamber and saidapparatus further comprising at least one particle withdrawal means influid communication with said flow reversal means from transporting saidsolid particles separated in said flow reversal means from saidseparation means.
 8. The apparatus of claim 2 wherein said inlet meansincludes at least one flow reversal means to substantially change thedirection of flow of said mixture prior to said mixture entering saidchamber to thereby cause at least a portion of said solid particles tobe separated from said mixture prior to said mixture entering saidchamber and said apparatus further comprising at least one particlewithdrawal means in fluid communication with said flow reversal meansfrom transporting said solid particles separated in said flow reversalmeans from said separation means.
 9. The apparatus of claim 4 whereinsaid inlet means includes at least one flow reversal means tosubstantially change the direction of flow of said mixture prior to saidmixture entering said chamber to thereby cause at least a portion ofsaid solid particles to be separated from said mixture prior to saidmixture entering said chamber and said apparatus further comprising atleast one particle withdrawal means in fluid communication with saidflow reversal means from transporting said solid particles separated insaid flow reversal means from said separation means.
 10. The apparatusof claim 6 wherein said inlet means includes at least one flow reversalmeans to substantially change the direction of flow of said mixtureprior to said mixture entering said chamber to thereby cause at least aportion of said solid particles to be separated from said mixture priorto said mixture entering said chamber and said apparatus furthercomprising at least one particle withdrawal means in fluid communicationwith said flow reversal means from transporting said solid particlesseparated in said flow reversal means from said separation means. 11.The apparatus of claim 1 wherein said inlet means includes at least oneflow directing means located in spaced relation to said interiorcylindrical surface acting to direct the flow of said mixture in saidchamber so that at least a portion of said solid particles movepreferentially toward said cylindrical surface.
 12. The apparatus ofclaim 2 wherein said inlet means includes at least one flow directingmeans located in spaced relation to said interior cylindrical surfaceacting to direct the flow of said mixture in said chamber so that atleast a portion of said solid particles move preferentially toward saidcylindrical surface.
 13. The apparatus of claim 4 wherein said inletmeans includes at least one flow directing means located in spacedrelation to said interior cylindrical surface acting to direct the flowof said mixture in said chamber so that at least a portion of said solidparticles move preferentially toward said cylindrical surface.
 14. Theapparatus of claim 6 wherein said inlet means includes at least one flowdirecting means located in spaced relation to said interior cylindricalsurface acting to direct the flow of said mixture in said chamber sothat at least a portion of said solid particles move preferentiallytoward said cylindrical surface.
 15. The apparatus of claim 1 whereinsaid separation means further comprises at least one plate means locatedin spaced relation to said interior cylindrical surface between saidinlet means and said particle outlet means for collecting at least aportion of said solid particles separated from said mixture in saidseparation means upstream from said plate means and transport means influid communication with said plate means for transporting at least aportion of said solid particles collected by said plate means from saidseparation means.
 16. The apparatus of claim 2 wherein said separationmeans further comprises at least one plate means located in spacedrelation to said interior cylindrical surface between said inlet meansand said particle outlet means for collecting at least a portion of saidsolid particles separated from said mixture in said separation meansupstream from said plate means and transport means in fluidcommunication with said plate means for transporting at least a portionof said solid particles collected by said plate means from saidseparation means.
 17. The apparatus of claim 4 wherein said separationmeans further comprises at least one plate means located in spacedrelation to said interior cylindrical surface between said inlet meansand said particle outlet means for collecting at least a portion of saidsolid particles separated from said mixture in said separation meansupstream from said plate means and transport means in fluidcommunication with said plate means for transporting at least a portionof said solid particles collected by said plate means from saidseparation means.
 18. The apparatus of claim 6 wherein said separationmeans further comprises at least one plate means located in spacedrelation to said interior cylindrical surface between said inlet meansand said particle outlet means for collecting at least a portion of saidsolid particles separated from said mixture in said separation meansupstream from said plate means and transport means in fluidcommunication with said plate means for transporting at least a portionof said solid particles collected by said plate means from saidseparation means.
 19. The apparatus of claim 1 wherein said separationmeans further comprises at least one velocity altering means located inspaced relation to said interior cylindrical surface downstream fromsaid inlet means to change the radial component of the velocity of themixture of solid particles and vapor flowing past said velocity alteringmeans.
 20. The apparatus of claim 2 wherein said separation meansfurther comprises at least one velocity altering means located in spacedrelation to said interior cylindrical surface downstream from said inletmeans to change the radial component of the velocity of the mixture ofsolid particles and vapor flowing past said velocity altering means. 21.The apparatus of claim 4 wherein said separation means further comprisesat least one velocity altering means located in spaced relation to saidinterior cylindrical surface downstream from said inlet means to changethe radial component of the velocity of the mixture of solid particlesand vapor flowing past said velocity altering means.
 22. The apparatusof claim 6 wherein said separation means further comprises at least onevelocity altering means located in spaced relation to said interiorcylindrical surface downstream from said inlet means to change theradial component of the velocity of the mixture of solid particles andvapor flowing past said velocity altering means.
 23. The apparatus ofclaim 19 wherein said separation means further comprises at least oneplate means located in spaced relation to said interior cylindricalsurface between said inlet means and said velocity altering means forcollecting at least a portion of said solid particles separated fromsaid mixture in said separation means upstream from said plate means andtransport means in fluid communication with said plate means fortransporting at least a portion of said solid particles collected bysaid plate means from said separation means.
 24. The apparatus of claim20 wherein said separation means further comprises at least one platemeans located in spaced relation to said interior cylindrical surfacebetween said inlet means and said velocity altering means for collectingat least a portion of said solid particles separated from said mixturein said separation means upstream from said plate means and transportmeans in fluid communication with said plate means for transporting atleast a portion of said solid particles collected by said plate meansfrom said separation means.
 25. The apparatus of claim 21 wherein saidseparation means further comprises at least one plate means located inspaced relation to said interior cylindrical surface between said inletmeans and said velocity altering means for collecting at least a portionof said solid particles separated from said mixture in said separationmeans upstream from said plate means and transport means in fluidcommunication with said plate means for transporting at least a portionof said solid particles collected by said plate means from saidseparation means.
 26. The apparatus of claim 22 wherein said separationmeans further comprises at least one plate means located in spacedrelation to said interior cylindrical surface between said inlet meansand said velocity altering means for collecting at least a portion ofsaid solid particles separated from said mixture in said separationmeans upstream from said plate means and transport means in fluidcommunication with said plate means for transporting at least a portionof said solid particles collected by said plate means from saidseparation means.
 27. In an apparatus for carrying out chemicalconversion of a feedstock which includes a chemical reaction zonewherein said feedstock is contacted with solid particles capable ofpromoting said chemical conversion at chemical conversion conditions toform at least one chemical conversion product and a mixture of solidparticles and vapor, the major portion by weight of said solid particleshaving diameters in the range from about 10 to about 500 microns; and atleast one separation means in fluid communication with said reactionzone wherein said mixture is at least partially separated, saidseparation means comprising a chamber defined by an interior cylindricalsurface; an inlet means in fluid communication with both sad reactionzone and said chamber to allow entry of said mixture to said chamber,said inlet means being situated so that movement of said mixture in saidchamber causes solid particles to preferentially move toward saidcylindrical surface; a fluid outlet means in fluid communication withsaid chamber to allow at least a portion of said vapor component of saidmixture to exit from said chamber; and a particle outlet means in fluidcommunication with said chamber to allow at least a portion of saidsolid particles to exit from said chamber; the improvement whichcomprises:at least one flow reversal means as a component of said inletmeans to substantially reverse the direction of flow of said mixtureprior to said mixture entering said chamber to thereby cause at least aportion of said solid particles to be separated from said mixture priorto said mixture entering said chamber, thereby inhibiting the attritionof said solid particles.
 28. The apparatus of claim 27 wherein saidapparatus further comprising at least one particle withdrawal means influid communication with said flow reversal means for transporting saidsolid particles separated in said flow reversal means from saidseparation means.
 29. The apparatus of claim 28 wherein said particlewithdrawal means is fluid communication with said particle outlet means.30. In an apparatus for carrying out chemical conversion of a feedstockwhich includes a chemical reaction zone wherein said feedstock iscontacted with solid particles capable of promoting said chemicalconversion at chemical conversion conditions to form at least onechemical conversion product and a mixture of solid particles and vapor,the major portion by weight of said solid particles having diameters inthe range from about 10 to about 500 microns; and at least oneseparation means in fluid communication with said reaction zone whereinsaid mixture is at least partially separated, said separation meanscomprising a chamber defined by an interior cylindrical surface; aninlet means in fluid communication with both said reaction zone and saidchamber to allow entry of said mixture to said chamber, said inlet meansbeing situated so that the movement of said mixture in said chambercauses solid particles to preferentially move toward said cylindricalsurface; a fluid outlet means in fluid communication with said chamberto allow at least a portion of said vapor component of said mixture toexit from said chamber; and a particle outlet means in fluidcommunication with said chamber to allow at least a portion of saidsolid particles to exit from said chamber; the improvement whichcomprises:at least one plate means located in spaced relation to saidinterior cylindrical surface between said inlet means and said particleoutlet means for collecting at least a portion of said solid particlesseparated from said mixture in said separation means upstream from saidplate means and transport means in fluid communication with said platemeans for transporting at least a portion of said solid particlescollected by said plate means from said separation means.
 31. Theapparatus of claim 30 wherein said plate means is attached to saidcylindrical surface and said transport means is in fluid communicationwith said particle outlet means.
 32. The apparatus of claim 30 whereinsaid separation means further comprises at least one velocity alteringmeans located in spaced relation to said interior cylindrical surfacedownstream from said plate means to change the radial component of thevelocity of said mixture of solid particles and vapor flowing past saidvelocity altering means.
 33. In an apparatus for restoring the catalyticactivity of solid particles which have previously been used to promotechemical conversion and have deactivating carbonaceous deposit materialthereon, the major portion by weight of said solid particles havingdiameters in the range from about 10 to about 500 microns which includesa regeneration zone wherein said deposit-containing solid particles arecontacted with oxygen-containing vapor at conditions to combust at leasta portion of said deposit material and form a mixture of solid particlesand vapor, and at least one separation means in fluid communication withsaid regeneration zone wherein said mixture is at least partiallyseparated, said separation means comprising a chamber defined by aninterior cylindrical surface; an inlet means to said chamber in fluidcommunication with both said regeneration zone and said chamber to allowentry of said mixture to said chamber, said inlet means being situatedso that the movement of said mixture in said chamber causes solidparticles to preferentially move toward said cylindrical surface, afluid outlet means in fluid communication with said chamber to allow atleast a portion of said vapor component of said mixture to exit fromsaid chamber; and a particle outlet means in fluid communication withsaid chamber to allow at least a portion of said solid particles to exitfrom said chamber; the improvement which comprises:arresting meanslocated in spaced relation to said interior cylindrical surface to slowthe velocity of at least a portion of said solid particles as saidparticles preferentially move toward said cylindrical surface, therebyinhibiting the attrition of said solid particles.
 34. The apparatus ofclaim 33 wherein said arresting means comprises a plurality of vanesattached to said cylindrical surface and which extend inwardly towardthe central axis of said chamber.
 35. The apparatus of claim 34 whereinsaid vanes which are mutually adjacent form a channel into which flowsat least a portion of said solid particles preferentially moving towardsaid cylindrical surface.
 36. The apparatus of claim 35 wherein saidvanes are attached to said cylindrical surface and are positioned sothat each said vane overlaps at least one adjacent vane when viewed fromthe central axis of said chamber.
 37. The apparatus of claim 36 whereineach of said vanes is inclined at an angle relative to said central axisof said chamber to reduce the resistance to flow of said solid particlesand vapor in said chamber caused by said vanes.
 38. The apparatus ofclaim 37 wherein each of said vanes extends a substantially equaldistance into said chamber so that the end of each of said vanes awayfrom said cylindrical surface is at a substantially equal distance fromsaid central axis of said chamber and each of said vanes is inclined ata substantially uniform angle relative to said central axis of saidchamber.
 39. The apparatus of claim 33 wherein said inlet means includesat least one flow reversal means to substantially change the directionof flow of said mixture prior to said mixture entering said chamber tothereby cause at least a portion of said solid particles to be separatedfrom said mixture prior to said mixture entering said chamber and saidapparatus further comprising at least one particle withdrawal means influid communication with said flow reversal means from transporting saidsolid particles separated in said flow reversal means from saidseparation means.
 40. The apparatus of claim 34 wherein said inlet meansincludes at least one flow reversal means to substantially change thedirection of flow of said mixture prior to said mixture entering saidchamber to thereby cause at least a portion of said solid particles tobe separated from said mixture prior to said mixture entering saidchamber and said apparatus further comprising at least one particlewithdrawal means in fluid communication with said flow reversal meansfrom transporting said solid particles separated in said flow reversalmeans from said separation means.
 41. The apparatus of claim 36 whereinsaid inlet means includes at least one flow reversal means tosubstantially change the direction of flow of said mixture prior to saidmixture entering said chamber to thereby cause at least a portion ofsaid solid particles to be separated from said mixture prior to saidmixture entering said chamber and said apparatus further comprising atleast one particle withdrawal means in fluid communication with saidflow reversal means from transporting said solid particles separated insaid flow reversal means from said separation means.
 42. The apparatusof claim 33 wherein said inlet means includes at least one flowdirecting means located in spaced relation to said interior cylindricalsurface acting to direct the flow of said mixture in said chamber sothat at least a portion of said solid particles move preferentiallytoward said cylindrical surface.
 43. The apparatus of claim 34 whereinsaid inlet means includes at least one flow directing means located inspaced relation to said interior cylindrical surface acting to directthe flow of said mixture in said chamber so that at least a portion ofsaid solid particles move preferentially toward said cylindricalsurface.
 44. The apparatus of claim 36 wherein said inlet means includesat least one flow directing means located in spaced relation to saidinterior cylindrical surface acting to direct the flow of said mixturein said chamber so that at least a portion of said solid particles movepreferentially toward said cylindrical surface.
 45. The apparatus ofclaim 33 wherein said separation means further comprises at least oneplate means located in spaced relation to said interior cylindricalsurface between said inlet means and said particle outlet means forcollecting at least a portion of said solid particles separated fromsaid mixture in said separation means upstream from said plate means andtransport means in fluid communication with said plate means fortransporting at least a portion of said solid particles collected bysaid plate means from said separation means.
 46. The apparatus of claim34 wherein said separation means further comprises at least one platemeans located in spaced relation to said interior cylindrical surfacebetween said inlet means and said particle outlet means for collectingat least a portion of said solid particles separated from said mixturein said separation means upstream from said plate means and transportmeans in fluid communication with said plate means for transporting atleast a portion of said solid particles collected by said plate meansfrom said separation means.
 47. The apparatus of claim 36 wherein saidseparation means further comprises at least one plate means located inspaced relation to said interior cylindrical surface between said inletmeans and said particle outlet means for collecting at least a portionof said solid particles separated from said mixture in said separationmeans upstream from said plate means and transport means in fluidcommunication with said plate means for transporting at least a portionof said solid particles collected by said plate means from saidseparation means.
 48. The apparatus of claim 33 wherein said separationmeans further comprises at least one velocity altering means located inspaced relation to said interior cylindrical surface downstream fromsaid inlet means to change the radial component of the velocity of themixture of solid particles and vapor flowing past said velocity alteringmeans.
 49. The apparatus of claim 34 wherein said separation meansfurther comprises at least one velocity altering means located in spacedrelation to said interior cylindrical surface downstream from said inletmeans to change the radial component of the velocity of the mixture ofsolid particles and vapor flowing past said velocity altering means. 50.The apparatus of claim 36 wherein said separation means furthercomprises at least one velocity altering means located in spacedrelation to said interior cylindrical surface downstream from said inletmeans to change the radial component of the velocity of the mixture ofsolid particles and vapor flowing past said velocity altering means. 51.The apparatus of claim 48 wherein said separation means furthercomprises at least one plate means located in spaced relation to saidinterior cylindrical surface between said inlet means and said velocityaltering means for collecting at least a portion of said solid particlesseparated from said mixture in said separation means upstream from saidplate means and transport means in fluid communication with said platemeans for transporting at least a portion of said solid particlescollected by said plate means from said separation means.
 52. Theapparatus of claim 49 wherein said separation means further comprises atleast one plate means located in spaced relation to said interiorcylindrical surface between said inlet means and said velocity alteringmeans for collecting at least a portion of said solid particlesseparated from said mixture in said separation means upstream from saidplate means and transport means in fluid communication with said platemeans for transporting at least a portion of said solid particlescollected by said plate means from said separation means.
 53. Theapparatus of claim 50 wherein said separation means further comprises atleast one plate means located in spaced relation to said interiorcylindrical surface between said inlet means and said velocity alteringmeans for collecting at least a portion of said solid particlesseparated from said mixture in said separation means upstream from saidplate means and transport means in fluid communication with said platemeans for transporting at least a portion of said solid particlescollected by said plate means from said separation means.
 54. In anapparatus for restoring the catalytic activity of solid particles whichhave previously been used to promote chemical conversion and havedeactivating carbonaceous deposit material thereon, the major portion byweight of said solid particles having diameters in the range from about10 to about 500 microns which includes a regeneration zone wherein saiddeposit-containing solid particles are contacted with oxygen-containingvapor at conditions to combust at least a portion of said depositmaterial and form a mixture of solid particles and vapor, and at leastone separation means in fluid communication with said regeneration zonewherein said mixture is at least partially separated, said separationmeans comprising a chamber defined by an interior cylindrical surface;an inlet means to said chamber in fluid communication with both saidregeneration zone and said chamber to allow entry of said mixture tosaid chamber, said inlet means being situated so that the movement ofsaid mixture in said chamber causes solid particles to preferentiallymove toward said cylindrical surface; a fluid outlet means in fluidcommunication with said chamber to allow at least a portion of saidvapor component of said mixture to exit from said chamber; and aparticle outlet means in fluid communication with said chamber to allowat least a portion of said solid particles to exit from said chamber;the improvement which comprises:at least one flow reversal means as acomponent of said inlet means to substantially reverse the direction offlow of said mixture prior to said mixture entering said chamber tothereby cause at least a portion of said solid particles to be separatedfrom said mixture prior to said mixture entering said chamber, therebyinhibiting the attrition of said solid particles.
 55. The apparatus ofclaim 54 wherein said apparatus further comprising at least one particlewithdrawal means in fluid communication with said flow reversal meansfor transporting said solid particles separated in said flow reversalmeans from said separation means.
 56. The apparatus of claim 55 whereinsaid particle withdrawal means is in fluid communication with saidparticle outlet means.
 57. In an apparatus for restoring the catalyticactivity of solid particles which have previously been used to promotechemical conversion and have deactivating carbonaceous deposit materialthereon, the major portion by weight of said solid particles havingdiameters in the range from about 10 to about 500 microns which includesa regeneration zone wherein said deposit-containing solid particles arecontacted with oxygen-containing vapor at conditions to combust at leasta portion of said deposit material and form a mixture of solid particlesand vapor, and at least one separation means in fluid communication withsaid regeneration zone wherein said mixture is at least partiallyseparated, said separation means comprising a chamber defined by aninterior cylindrical surface; an inlet means to said chamber in fluidcommunication with both said regeneration zone and said chamber to allowentry of said mixture to said chamber, said inlet means being situatedso that the movement of said mixture in said chamber causes solidparticles to preferentially move toward said cylindrical surface; afluid outlet means in fluid communication with said chamber to allow atleast a portion of said vapor component of said mixture to exit fromsaid chamber; and a particle outlet means in fluid communication withsaid chamber to allow at least a portion of said solid particles to exitfrom said chamber; the improvement which comprises:at least one platemeans located in spaced relation to said interior cylindrical surfacebetween said inlet means and said particle outlet means for collectingat least a portion of said solid particles separated from said mixturein said separation means upstream from said plate means and transportmeans in fluid communication with said plate means for transporting atleast a portion of said solid particles collected by said plate meansfrom said separation means.
 58. The apparatus of claim 57 wherein saidplate means is attached to said cylindrical surface and said transportmeans is in fluid communication with said particle outlet means.
 59. Theapparatus of claim 57 wherein said separation means further comprises atleast one velocity altering means located in spaced relation to saidinterior cylindrical surface downstream from said plate means to changethe radial component of the velocity of said mixture of solid particlesand vapor flowing past said velocity altering means.
 60. In an apparatusfor at least partially separating a mixture of solid particles and vaporincluding a chamber defined by an interior cylindrical surface; an inletmeans in fluid communication with said chamber to allow entry of saidmixture to said chamber, said inlet means being situated so that themovement of said mixture in said chamber causes solid particles topreferentially move toward said cylindrical surface; a fluid outletmeans in fluid communication with said chamber to allow at least aportion of said vapor component of said mixture to exit from saidchamber; and a particle outlet means in fluid communication with saidchamber to allow at least a portion of said solid particles to exit fromsaid chamber; the improvement which comprises a plurality of vanesattached to said interior cylindrical surface to slow the velocity of atleast a portion of said solid particles as said solid particlespreferentially move toward said cylindrical surface, thereby inhibitingthe attrition of said solid particles, said vanes being positioned sothat each said vane overlaps at least one adjacent vane when viewed fromthe central axis of said chamber.
 61. The apparatus of claim 60 whereineach of said vanes extends a substantially equal distance into saidchamber so that the end of each of said vanes away from said cylindricalsurface is at a substantially equal distance from said central axis ofsuch chamber.
 62. The apparatus of claim 60 wherein each of said vanesis inclined at an angle relative to said central axis of said chamber toreduce the resistance to flow of said solid particles and vapor in saidchamber caused by said vanes.
 63. The apparatus of claim 61 wherein eachof said vanes is inclined at an angle relative to said central axis ofsaid chamber to reduce the resistance to flow of said solid particlesand vapor in said chamber caused by said vanes.
 64. The apparatus ofclaim 60 wherein said inlet means includes at least one flow reversalmeans to substantially change the direction of flow of said mixtureprior to said mixture entering said chamber to thereby cause at least aportion of said solid particles to be separated from said mixture priorto said mixture entering said chamber and said apparatus furthercomprising at least one particle withdrawal means in fluid communicationwith said flow reversal means from transporting said solid particlesseparated in said flow reversal means from said separation means. 65.The apparatus of claim 63 wherein said inlet means includes at least oneflow reversal means to substantially change the direction of flow ofsaid mixture prior to said mixture entering said chamber to therebycause at least a portion of said solid particles to be separated fromsaid mixture prior to said mixture entering said chamber and saidapparatus further comprising at least one particle withdrawal means influid communication with said flow reversal means from transporting saidsolid particles separated in said flow reversal means from saidseparation means.
 66. The apparatus of claim 60 wherein said inlet meansincludes at least one flow directing means located in spaced relation tosaid interior cylindrical surface acting to direct the flow of saidmixture in said chamber so that at least a portion of said solidparticles move preferentially toward said cylindrical surface.
 67. Theapparatus of claim 63 wherein said inlet means includes at least oneflow directing means located in spaced relation to said interiorcylindrical surface acting to direct the flow of said mixture in saidchamber so that at least a portion of said solid particles movepreferentially toward said cylindrical surface.
 68. The apparatus ofclaim 60 wherein said separation means further comprises at least oneplate means located in spaced relation to said interior cylindricalsurface between said inlet means and said particle outlet means forcollecting at least a portion of said solid particles separated fromsaid mixture in said separation means upstream from said plate means andtransport means in fluid communication with said plate means fortransporting at least a portion of said solid particles collected bysaid plate means from said separation means.
 69. The apparatus of claim63 wherein said separation means further comprises at least one platemeans located in spaced relation to said interior cylindrical surfacebetween said inlet means and said particle outlet means for collectingat least a portion of said solid particles separated from said mixturein said separation means upstream from said plate means and transportmeans in fluid communication with said plate means for transporting atleast a portion of said solid particles collected by said plate meansfrom said separation means.
 70. The apparatus of claim 60 wherein saidseparation means further comprises at least one velocity altering meanslocated in spaced relation to said interior cylindrical surfacedownstream from said inlet means to change the radial component of thevelocity of the mixture of solid particles and vapor flowing past saidvelocity altering means.
 71. The apparatus of claim 63 wherein saidseparation means further comprises at least one velocity altering meanslocated in spaced relation to said interior cylindrical surfacedownstream from said inlet means to change the radial component of thevelocity of the mixture of solid particles and vapor flowing past saidvelocity altering means.
 72. The apparatus of claim 70 wherein saidseparation means further comprises at least one plate means located inspaced relation to said interior cylindrical surface between said inletmeans and said velocity altering means for collecting at least a portionof said solid particles separated from said mixture in said separationmeans upstream from said plate means and transport means in fluidcommunication with said plate means for transporting at least a portionof said solid particles collected by said plate means from saidseparation means.
 73. In a method for at least partially separating amixture of solid particles and vapor into separate solid (1) particlesand (2) vapor, the improvement which comprises causing said mixture toflow into the apparatus of claim
 60. 74. In a method for at leastpartially separating a mixture of solid particles and vapor intoseparate solid (1) particles and (2) vapor, the improvement whichcomprises causing said mixture to flow into the apparatus of claim 63.75. In a method for at least partially separating a mixture of solidparticles and vapor into separate solid (1) particles and (2) vapor, theimprovement which comprises causing said mixture to flow into theapparatus of claim
 64. 76. In a method for at least partially separatinga mixture of solid particles and vapor into separate solid (1) particlesand (2) vapor, the improvement which comprises causing said mixture toflow into the apparatus of claim
 66. 77. In a method for at leastpartially separating a mixture of solid particles and vapor intoseparate solid (1) particles and (2) vapor, the improvement whichcomprises causing said mixture to flow into the apparatus of claim 68.78. In a method for at least partially separating a mixture of solidparticles and vapor into separate solid (1) particles and (2) vapor, theimprovement which comprises causing said mixture to flow into theapparatus of claim
 70. 79. In an apparatus for at least partiallyseparating a mixture of solid particles and vapor including a chamberdefined by an interior cylindrical surface; an inlet means in fluidcommunication with said chamber to allow entry of said mixture to saidchamber, said inlet means being situated so that the movement of saidmixture in said chamber causes solid particles to preferentially movetoward said cylindrical surface; a fluid outlet means in fluidcommunication with said chamber to allow at least a portion of saidvapor component of said mixture to exit from said chamber; and aparticle outlet means in fluid communication with said chamber to allowat least a portion of said solid particles to exit from said chamber;the improvement which comprises a plurality of vanes attached to saidinterior cylindrical surface to slow the velocity of at least a portionof said solid particles as said solid particles preferentially movetoward said cylindrical surface, thereby inhibiting the attrition ofsaid solid particles, each of said vanes being inclined at an anglerelative to said central axis of said chamber to reduce the resistanceto flow of said solid particles and vapor in said chamber caused by saidvanes.
 80. The apparatus of claim 79 wherein each of said vanes isinclined at a substantially uniform angle relative to said central axis.81. The apparatus of claim 79 wherein said vanes are positioned so thateach said vane overlaps at least one adjacent vane when viewed from thecentral axis of said chamber.
 82. The apparatus of claim 80 wherein saidvanes are positioned so that each said vane overlaps at least oneadjacent vane when viewed from the central axis of said chamber.
 83. Theapparatus of claim 79 wherein said inlet means includes at least oneflow reversal means to substantially change the direction of flow ofsaid mixture prior to said mixture entering said chamber to therebycause at least a portion of said solid particles to be separated fromsaid mixture prior to said mixture entering said chamber and saidapparatus further comprising at least one particle withdrawal means influid communication with said flow reversal means from transporting saidsolid particles separated in said flow reversal means from saidseparation means.
 84. The apparatus of claim 82 wherein said inlet meansincludes at least one flow reversal means to substantially change thedirection of flow of said mixture prior to said mixture entering saidchamber to thereby cause at least a portion of said solid particles tobe separated from said mixture prior to said mixture entering saidchamber and said apparatus further comprising at least one particlewithdrawal means in fluid communication with said flow reversal meansfrom transporting said solid particles separated in said flow reversalmeans from said separation means.
 85. The apparatus of claim 79 whereinsaid inlet means includes at least one flow directing means located inspaced relation to said interior cylindrical surface acting to directthe flow of said mixture in said chamber so that at least a portion ofsaid solid particles move preferentially toward said cylindricalsurface.
 86. The apparatus of claim 82 wherein said inlet means includesat least one flow directing means located in spaced relation to saidinterior cylindrical surface acting to direct the flow of said mixturein said chamber so that at least a portion of said solid particles movepreferentially toward said cylindrical surface.
 87. The apparatus ofclaim 79 wherein said separation means further comprises at least oneplate means located in spaced relation to said interior cylindricalsurface between said inlet means and said particle outlet means forcollecting at least a portion of said solid particles separated fromsaid mixture in said separation means upstream from said plate means andtransport means in fluid communication with said plate means fortransporting at least a portion of said solid particles collected bysaid plate means from said separation means.
 88. The apparatus of claim82 wherein said separation means further comprises at least one platemeans located in spaced relation to said interior cylindrical surfacebetween said inlet means and said particle outlet means for collectingat least a portion of said solid particles separated from said mixturein said separation means upstream from said plate means and transportmeans in fluid communication with said plate means for transporting atleast a portion of said solid particles collected by said plate meansfrom said separation means.
 89. The apparatus of claim 79 wherein saidseparation means further comprises at least one velocity altering meanslocated in spaced relation to said interior cylindrical surfacedownstream from said inlet means to change the radial component of thevelocity of the mixture of solid particles and vapor flowing past saidvelocity altering means.
 90. The apparatus of claim 82 wherein saidseparation means further comprises at least one velocity altering meanslocated in spaced relation to said interior cylindrical surfacedownstream from said inlet means to change the radial component of thevelocity of the mixture of solid particles and vapor flowing past saidvelocity altering means.
 91. The apparatus of claim 89 wherein saidseparation means further comprises at least one plate means located inspaced relation to said interior cylindrical surface between said inletmeans and said velocity altering means for collecting at least a portionof said solid particles separated from said mixture in said separationmeans upstream from said plate means and transport means in fluidcommunication with said plate means for transporting at least a portionof said solid particles collected by said plate means from saidseparation means.
 92. In a method for at least partially separating amixture of solid particles and vapor into separate solid (1) particlesand (2) vapor, the improvement which comprises causing said mixture toflow into the apparatus of claim
 79. 93. In a method for at leastpartially separating a mixture of solid particles and vapor intoseparate solid (1) particles and (2) vapor, the improvement whichcomprises causing said mixture to flow into the apparatus of claim 82.94. In a method for at least partially separating a mixture of solidparticles and vapor into separate solid (1) particles and (2) vapor, theimprovement which comprises causing said mixture to flow into theapparatus of claim
 83. 95. In a method for at least partially separatinga mixture of solid particles and vapor into separate solid (1) particlesand (2) vapor, the improvement which comprises causing said mixture toflow into the apparatus of claim
 85. 96. In a method for at leastpartially separating a mixture of solid particles and vapor intoseparate solid (1) particles and (2) vapor, the improvement whichcomprises causing said mixture to flow into the apparatus of claim 87.97. In a method for at least partially separating a mixture of solidparticles and vapor into separate solid (1) particles and (2) vapor, theimprovement which comprises causing said mixture to flow into theapparatus of claim 89.